Background of the Invention
[0001] This invention relates to an improved process for selectively removing hydrogen sulfide
from gaseous streams. More particularly, this invention relates to an improved process
for selectively removing hydrogen sulfide from gaseous streams containing less than
500 ppm free hydrogen, by contacting said gaseous streams with a nickel-promoted absorbing
composition.
[0002] The removal of sulfur from fluid streams can be desirable or necessary for a variety
of reasons. If the fluid stream is to be released as a waste stream, removal of sulfur
from the fluid stream can be necessary to meet the sulfur emmission requirements set
by various air pollution control authorities. Such requirements are generally in the
range of about 10 ppm to 500 ppm of sulfur in the fluid stream. If the fluid stream
is to be burned as a fuel, removal of sulfur from the fluid stream can be necessary
to prevent environmental pollution. If the fluid stream is to be processed, removal
of the sulfur is often necessary to prevent the poisoning of sulfur sensitive catalysts
or to satisfy other process requirements.
[0003] A variety of methods employing regenerable, solid contact materials are known for
removing sulfur from a fluid stream when the sulfur is present as hydrogen sulfide.
For example, United States Patent Number 4,371,728 discloses a composition comprising
zinc, titanium and at least one metal promoter which is an effective absorbing composition
for hydrogen sulfide and which possesses the property of being regenerable to the
original absorbing composition state in the presence of oxygen when fully sulfided.
Also, United States Patent Number 4,725,415 discloses a composition comprising zinc
titanate, alumina, at least one metal promoter selected from tungsten and molybdenum,
and at least one metal promoter selected from Group VIII of the Periodic Table which
is an effective absorbing composition for hydrogen sulfide and which possesses the
property of being regenerable to the original absorbing composition state in the presence
of oxygen when fully sulfided.
[0004] Although the compositions disclosed in these United States patents are effective
absorbing compositions for hydrogen sulfide, it has been found that when the hydrogen
sulfide containing fluid stream has a free hydrogen content below about 500 ppm, many
of the promoting metals employed in these compositions effectively oxidize significant
amounts of the hydrogen sulfide to sulfur dioxide. The resulting sulfur dioxide is
not absorbed by these patented compositions and, thus, passes unabsorbed through the
contact material. In view of the fact that environmental concerns are focused on the
total amount of sulfur contained in an effluent stream, and not just the amount of
hydrogen sulfide, passing sulfur dioxide through the contact material and out to the
environment is not acceptable under current environmental standards.
Summary of the Invention
[0005] It is thus an object of the present invention to provide an improved absorbing composition
for selectively removing hydrogen sulfide from fluid streams containing hydrogen sulfide
and less than 500 ppm of free hydrogen without producing a treated fluid stream containing
significant amounts of sulfur dioxide. It is a further object of this invention to
provide an improved removal or absorbing composition which possesses the property
of being regenerable to the original absorbing composition state in the presence of
oxygen when fully sulfided.
[0006] It has been found, in accordance with the present invention, that nickel oxide will
not oxidize hydrogen sulfide to sulfur dioxide when contacted with a fluid stream
containing hydrogen sulfide and less than 500 ppm of free hydrogen under the conditions
of the process of the present invention. An absorbing composition promoted only with
nickel oxide will, however, effectively absorb substantially all of the hydrogen sulfide
contained in such a fluid stream.
Detailed Description of the Invention
[0007] Thus, in accordance with the present invention, an absorbing composition consisting
essentially of a base material and nickel oxide is utilized to selectively remove
hydrogen sulfide from a fluid stream containing hydrogen sulfide and less than 500
ppm of free hydrogen. The base material is selected from the group consisting of zinc
oxide and zinc titanate, preferably combined with alumina. Once the absorbing composition
of the present invention has been prepared, fluid streams containing hydrogen sulfide
and less than 500 ppm of free hydrogen are contacted with the absorbing composition
under suitable absorbing conditions to substantially reduce the concentration of hydrogen
sulfide in the fluid stream without significantly increasing the concentration of
sulfur dioxide in the fluid stream.
[0008] It is believed that the hydrogen sulfide is being absorbed by the absorbing composition
and thus the terms "absorption process" and "absorbing composition" are utilized for
the sake of convenience. However, the exact chemical phenomenon occurring is not the
inventive feature of the process of the present invention and the use of the term
"absorb" in any form is not intended to limit the present invention.
[0009] The selective absorption process is preferably carried out in cycles comprising an
absorption period and a period for the regeneration of the sulfided absorbing composition.
The absorption period comprises contacting a gaseous stream which contains hydrogen
sulfide and less than 500 ppm of free hydrogen with the absorbing composition to thereby
selectively remove hydrogen sulfide from the gaseous stream. The absorbing composition
becomes sulfided during the absorption period. When the absorbing composition becomes
sulfided to the point that regeneration is desirable, preferably when it is nearly
completely sulfided, an oxygen-containing gas is passed in contact with the absorbing
composition to regenerate the absorbing composition and to convert the absorbed sulfur
to a sulfur oxide.
[0010] The chemical changes that are believed to occur in the absorbing composition during
this cyclic process are summarized in the following equations:
(I) Zn₂TiO₄ + 2H₂S → 2ZnS + TiO₂ + 2H₂O
(II) ZnS + Oxygen → ZnO + SO
x
(III) 2ZnO + TiO₂ → Zn₂TiO₄ or,
(IV) ZnO + H₂S → ZnS + H₂O
(V) ZnS + Oxygen → ZnO + SO
x and,
(VI) NiO + H₂S → NiS + H₂O
(VII) NiS + Oxygen → NiO + SO
x
[0011] Other objects and advantages of the invention will be apparent from the foregoing
description of the invention and the appended claims as well as from the detailed
description of the invention which follows.
[0012] The absorbing composition of the present invention may be utilized to remove hydrogen
sulfide from any suitable gaseous stream. The hydrogen sulfide may be produced by
the hydrodesulfurization of organic sulfur compounds or may be originally present
in the gaseous stream as hydrogen sulfide. Examples of such suitable gaseous streams
include light hydrocarbons, such as methane, ethane, and natural gas, and gases derived
from such light hydrocarbons; gases derived from petroleum products and products from
extraction and/or liquefaction of coal and lignite; gases derived from tar sands and
shale oil; coal derived synthesis gas; gases such as hydrogen and nitrogen; gaseous
oxides of carbon; steam; the inert gases such as helium and argon; and product gas
streams, from other hydrogen sulfide removal processes, that contain residual hydrogen
sulfide due to the incomplete removal of hydrogen sulfide by the prior process. Gases
that adversely affect the removal of hydrogen sulfide and which should be absent from
the gaseous streams being processed are oxidizing agents, examples of which include
air, molecular oxygen, the halogens, and the oxides of nitrogen.
[0013] Although the absorbing composition of the present invention is effective in the removal
of hydrogen sulfide from all suitable gaseous streams, it is especially effective
in the removal of hydrogen sulfide from gaseous streams that contain less than about
500 ppm of free hydrogen, wherein it is desirable not to promote the oxidation of
the hydrogen sulfide contained in such gaseous streams to sulfur dioxide. Examples
of such suitable gaseous streams include acid gas streams derived from methane, ethane,
and natural gas; olefin streams; and product gas streams, from other hydrogen sulfide
removal processes, that contain residual hydrogen sulfide due to the incomplete removal
of hydrogen sulfide by the prior process.
[0014] The absorbing composition of the present invention may be utilized to remove hydrogen
sulfide from olefins such as ethylene. This process, however, should be carried out
in the absence of free hydrogen to avoid hydrogenation. Olefin streams should not
be hydrodesulfurized as this may result in undesirable hydrogenation of at least a
portion of the olefins to paraffins.
[0015] The absorbing composition employed in the process of the present invention is a composition
consisting essentially of a base material selected from the group consisting of zinc
oxide and zinc titanate, preferably combined with alumina, and nickel oxide.
[0016] The absorbing composition employed in the process of the present invention may be
prepared by any suitable method known in the art. When the absorbing composition consists
essentially of zinc oxide and nickel oxide, or zinc titanate and nickel oxide, the
composition may be prepared by any method known in the art by which the nickel oxide
promoter may be combined with the zinc oxide or zinc titanate base material. Examples
of such methods include coprecipitation, incipient wettness impregnation, spray impregnation,
and solid mixing. These methods are well known in the art and therefore will not be
further discussed herein. Once the absorbing composition has been prepared, it may
be formed into a suitable contact material by any suitable method known in the art.
Examples of such suitable methods include extrusion, pelletization, tabletting, and
spray drying.
[0017] The zinc oxide used in the preparation of the absorbing composition may be either
in the form of zinc oxide, or in the form of one or more zinc compounds that are convertible
to zinc oxide under the conditions of preparation described herein. Examples of such
zinc compounds include zinc sulfide, zinc sulfate, zinc hydroxide, zinc carbonate,
zinc acetate, and zinc nitrate. Preferably, the zinc oxide is in the form of powdered
zinc oxide.
[0018] The zinc titanate used in the preparation of the absorbing composition is preferably
prepared in accordance with the methods disclosed in United States Patent Number 4,522,709
beginning on line 55 of column 2 and continuing to line 27 of column 3, which disclosure
is incorporated herein by reference.
[0019] When the absorbing composition employed in the process of the present invention consists
essentially of zinc titanate, alumina, and nickel oxide, the composition is preferably
prepared by first preparing zinc titanate which is then reduced to a small size. The
resulting zinc titanate is then mixed with a hydrosol of a suitable acidic material
comprising alumina. A suitable base is then added to the mixture to form a hydrogel.
The resulting hydrogel is dried slowly and calcined to form a hydrogel derived composition
of zinc titanate and alumina. Nickel oxide is then added to the hydrogel derived composition
of zinc titanate and alumina, and the promoted composition is again dried and calcined
to form the absorbing composition employed in the process of the present invention.
[0020] In accordance with this preferred method, zinc titanate is prepared in accordance
with the methods disclosed in U.S. 4,522,709 as previously discussed herein. The resulting
zinc titanate is then reduced to a size that is suitable for mixing with a hydrosol
of alumina. Any suitable method for reducing the particle size of the zinc titanate
to a size suitable for mixing with a hydrosol of alumina may be used. An example of
such a method is the treatment of the zinc titanate in an ultrasonic disrupter. The
zinc titanate may be reduced to any suitable size, with a particle size in the range
of about 1.0 micron to about 10 microns being preferred.
[0021] The resulting zinc titanate, having a fine particle size, is mixed with a hydrosol
of alumina. Any suitable form of alumina may be utilized. Alumina hydrate is particularly
preferred because a hydrosol of alumina hydrate is readily converted to a hydrogel
and then to the oxide phase after calcination.
[0022] After the zinc titanate has been thoroughly mixed into the hydrosol, a suitable base
is added to convert the hydrosol to a hydrogel. Any suitable base such as alkali metal
hydroxides, ammonium hydroxide, or urea may be utilized. Ammonium hydroxide is the
preferred base because it does not have any metallic component that would remain in
the hydrogel.
[0023] The resulting hydrogel is dried slowly so that water will not be removed so rapidly
that the hydrogel structure will collapse which would result in an excessive loss
of pore volume and surface area in the finished hydrogel derived absorbing composition.
Any suitable drying time can be utilized which does not result in too rapid a removal
of water. Preferably, the drying time is in the range of about 8 hours to about 24
hours.
[0024] Any suitable temperature can be utilized for the drying of the zinc titanate and
alumina hydrogel but again the temperature should be such that too rapid a removal
of water does not result. The temperature is preferably in the range of about 35°C
to about 150°C. The most preferred drying condition is to start the drying process
at about 80°C and increase the temperature slowly to about 120°C during the drying
time.
[0025] After the zinc titanate and alumina hydrogel has been dried, it is then calcined
in the presence of free oxygen to form the hydrogel derived absorbing composition.
Any suitable free oxygen-containing gas may be utilized, with air being preferred
because of its availability. Also, any suitable time and temperature for calcining
may be utilized with a preferred time being about two hours and a preferred temperature
being in the range of about 425°C to about 650°C and more preferably in the range
of about 480°C to about 600°C. Although the dried zinc titanate and alumina hydrogel
can be placed directly into a preheated furnace or kiln for calcining, it is preferable
for the hydrogel to attain its final temperature during a heating period of about
two hours.
[0026] When the absorbing composition employed in the process of the present invention consists
essentially of zinc oxide, alumina, and nickel oxide, the composition is preferably
prepared by initially mixing zinc oxide, alumina, and a dilute acid, thereby forming
a peptized composition of zinc oxide and alumina. The peptized composition of zinc
oxide and alumina is then dried and calcined to form the base material of the absorbing
composition. Nickel oxide or its precursor is then added to the base material, and
the promoted composition is again dried and calcined to form the absorbing composition
employed in the process of the present invention.
[0027] Alternatively, the nickel oxide or its precursor may be added to the zinc oxide and
alumina mixture during the formation of the peptized composition of zinc oxide and
alumina, thus reducing the number of times the composition must be dried and calcined
to form the absorbing composition.
[0028] In accordance with the preferred method described above, powdered zinc oxide and
alumina-hydrate are initially combined in a mixer. To achieve the desired dispersion
of these materials, the materials are blended until a homogeneous mixture is formed.
Generally, this mixing time will be in the range of about 1.0 minute to about 45 minutes,
and will preferably be in the range of about 2.0 minutes to about 15 minutes.
[0029] When the zinc oxide and alumina have been blended within the mixer for the desired
amount of time, a dilute acid is then added, with continued mixing, to the resulting
mixture to thereby form a peptized composition of zinc oxide and alumina. The dilute
acid may be added to the resulting mixture by any suitable method. Preferably, the
dilute acid is added to the resulting mixture by spraying it within the mixer during
continued mixing.
[0030] In an alternate embodiment of the present invention, the zinc oxide and alumina base
material is prepared by initially forming a hydrogel of zinc oxide and alumina. In
accordance with this embodiment, an alumina compound and a dilute acid are intitially
combined with stirring to form an acidic solution comprising alumina. Zinc oxide is
then added to the solution to form a hydrogel of zinc oxide and alumina.
[0031] Any suitable form of alumina may be used in the preparation of the absorbing composition
employed in the process of the present invention. Examples of suitable forms of alumina
include Gibbsite, Bayerite, and boehmite. Preferably, the alumina is in the form of
boehmite.
[0032] Any suitable acid may be used in the preparation of the absorbing composition. Examples
of suitable acids include nitric acid, acetic acid, sulfuric acid, and hydrochloric
acid, with acetic acid being presently preferred. The acid concentration in the dilute
acid employed in the preparation of the absorbing composition will generally be in
the range of about 1.0 weight-% to about 15 weight-%, and will preferably be in the
range of about 1.0 weight-% to about 5.0 weight-%, said weight-% being expressed in
terms of the weight of the concentrated acid based upon the total weight of the dilute
acid.
[0033] Regardless of which method is used to form the zinc oxide and alumina base material,
the resulting composition is then dried and calcined. Any suitable drying time can
be utilized to dry the composition of zinc oxide and alumina. The drying time is preferably
in the range of about 0.5 hour to about 4 hours, and is most preferably in the range
of about 1 hour to about 2 hours.
[0034] Any suitable temperature can be utilized to dry the composition of zinc oxide and
alumina. The drying temperature is preferably in the range of about 75°C to about
300°C, and is most preferably.in the range of about 90°C to about 250°C.
[0035] After the composition of zinc oxide and alumina is dried, it is then calcined in
the presence of free oxygen to form the base material for the absorbing composition
employed in the process of the present invention. Any suitable free oxygen-containing
gas may be utilized, with air being preferred because of its availability. Also, any
suitable time and temperature for calcining may be utilized. Generally, the calcination
time will be in the range of about 0.5 hour to about 4 hours, and will preferably
be in the range of about 1 hour to about 2 hours. The calcination temperature will
generally be in the range of about 375°C to about 750°C and will preferably be in
the range of about 500°C to about 700°C.
[0036] The absorbing compositions employed in the process of the present invention that
consist essentially of a base material selected from zinc oxide and zinc titanate,
alumina, and nickel oxide can contain any suitable amount of alumina. The amount of
alumina in these absorbing compositions will generally be in the range of about 10
weight-% to about 50 weight-%, and will more preferably be in the range of about 30
weight-% to about 40 weight-%, said weight-%'s being expressed in terms of the weight
of the alumina in comparison to the total weight of the absorbing composition.
[0037] Nickel oxide may be added to the absorbing composition of the present invention in
the form of elemental nickel, nickel oxide, and/or nickel-containing compounds that
are convertible to nickel oxides under the calcining conditions described herein.
Some examples of such nickel-containing compounds include nickel acetates, nickel
carbonates, nickel nitrates, nickel oxides, nickel sulfates, nickel thiocyanates,
and mixtures of two or more thereof.
[0038] The elemental nickel, nickel oxide, and/or nickel-containing compounds can be added
to the absorbing composition by any method known in the art. One such method is the
impregnation of the base material with a solution, either aqueous or organic, that
contains the elemental nickel, nickel oxide, and/or nickel-containing compounds. After
the elemental nickel, nickel oxide, and/or nickel-containing compounds have been added
to the base material, the resulting composition is dried and calcined, as described
hereinafter.
[0039] The elemental nickel, nickel oxide, and/or nickel-containing compounds can be included
as components in the preparation of the base materials, or they may be added to the
formed base materials after the base materials have initially been dried and calcined.
In the event the elemental nickel, nickel oxide, and/or nickel-containing compounds
are included during the preparation of the base material, then the base material is
formed, dried, and calcined in the manners previously describe herein.
[0040] In the event the elemental nickel, nickel oxide, and/or nickel-containing compounds
are added to the base material after it has initially been dried and calcined, then
the promoted base material is again dried and calcined following the addition of the
promoting metals. The promoted base material is generally dried at a temperature in
the range of about 75°C to about 300°C, more preferably in the range of about 90°C
to about 250°C, and for a drying time generally in the range of about 0.5 hour to
about 8 hours, more preferably in the range of about 3 hours to about 5 hours. The
dried, promoted base material is then calcined in the presence of free oxygen at a
temperature generally in the range of about 375°C to about 750°C, more preferably
in the range of about 500°C to about 700°C, until volatile matter is removed and the
elemental nickel and/or the nickel-containing compounds are substantially converted
to nickel oxides. The time required for this calcining step will generally range from
about 0.5 hour to about 4 hours, and will preferably be in the range of about 1 hour
to about 2 hours.
[0041] The nickel oxide will generally be present in the absorbing composition in an amount
ranging from about 0.1 weight-% to about 15 weight-%, and will more preferably be
in the range of about 2 weight-% to about 7.5 weight-%, said weight-%'s being expressed
in terms of nickel oxide based upon the total weight of the absorbing composition.
[0042] The processes of the present invention can be carried out by means of any apparatus
whereby there is achieved an alternate contact of the absorbing composition with the
gaseous feed stream and, thereafter, of the absorbing composition with an oxygen-containing
gas which is utilized to regenerate the absorbing composition. The process is in no
way limited to the use of a particular apparatus. The process of this invention can
be carried out using a fixed bed of absorbing composition, a fluidized bed of absorbing
composition, or a moving bed of absorbing composition. Presently preferred is a fixed
bed of absorbing composition.
[0043] In order to avoid any casual mixing of the gaseous feed stream containing hydrogen
sulfide with the oxygen-containing gas utilized in the regeneration step, provision
is preferably made for terminating the flow of the gaseous feed stream to the reactor
and subsequently injecting an inert purging fluid such as nitrogen, carbon dioxide
or steam. Any suitable purge time can be utilized but the purge should be continued
until all hydrocarbon and/or hydrogen sulfide are removed. Any suitable flow rate
of the purge fluid may be utilized. Presently preferred is a purge fluid flow rate
in the range of about 800 GHSV to about 1200 GHSV.
[0044] Any suitable temperature for the processes of the present invention may be utilized.
The temperature will generally be in the range of about 150°C to about 600°C and will
more preferably be in the range of about 200°C to about 450°C.
[0045] Any suitable temperature may be utilized to regenerate the absorbing composition
from its sulfided form back to the original absorbing composition form. The temperature
will generally be in the range of about 370°C to about 815°C. As part of this invention,
however, it has been discovered that the higher temperatures required to intiate the
regeneration of ZnS to ZnO (i.e. about 650°C and higher) has an adverse effect on
the amount of sulfur dioxide that is produced during the subsequent absorption cycle.
Due to the fact that the regeneration of NiS to NiO is an exothermic reaction, and
the fact that this reaction is initiated at a lower temperature (i.e. about 425°C),
the presence of nickel oxide in the absorbing composition employed in the process
of the present invention allows the regeneration to occur at a lower temperature,
thereby preventing the adverse effect describe above. Thus, the regeneration temperature
is preferably in the range of about 425°C to about 600°C, most preferably about 425°C,
to effect the regeneration within a reasonable time while not adversely affecting
the production of sulfur dioxide in the treated gaseous feed stream.
[0046] Any suitable pressure can be utilized for the processes of the present invention.
The pressure of the gaseous feed stream being treated is not believed to have an important
effect on the absorption process of the present invention, and will generally be in
the range of from about atmospheric to about 2,000 psig during the treatment.
[0047] Any suitable residence time for the gaseous feed stream in the presence of the absorbing
composition of the present invention can be utilized. The residence time expressed
as volumes of gas at standard temperature and pressure per volume of absorbing composition
per hour will generally be in the range of about 10 to about 10,000 and will more
preferably be in the range of about 250 to about 2500.
[0048] When the absorbing composition is completely sulfided it will no longer combine with
the hydrogen sulfide in the manner set forth in equations (I), (IV), and (VI). When
this condition occurs, hydrogen sulfide will begin to appear in the effluent flowing
from the reaction and this will be an indication that the absorbing composition should
preferably be regenerated. The time required for the absorbing composition to become
completely sulfided will generally be a function of the concentration of sulfur in
the feedstock and feed rate employed.
[0049] When the absorbing composition becomes substantially completely sulfided, the absorbing
composition is typically regenerated by terminating the flow of feed to the reactor
and purging with an inert fluid such as nitrogen to remove any combustibles. A free
oxygen-containing gas is then introduced to the reactor for the purpose of oxidizing
the zinc sulfide and the nickel sulfide in accordance with equations (II), (V), and
(VII). Also, with respect to the absorbing compositions containing zinc titanate,
at the temperature at which the oxidation of the zinc sulfide is effected, the zinc
oxide thus produced recombines with the titanium dioxide to resynthesize the original
zinc titanate in accordance with equation (III).
[0050] The amount of oxygen supplied to the reactor during the regeneration step will generally
be sufficient to at least substantially remove sulfur from the absorbing composition.
The regeneration step is generally conducted at about atmospheric pressure. The temperature
for the regeneration step is generally maintained in the range of about 370°C to about
815°C, and is more preferably maintained at about 425°C in order to both oxidize the
zinc sulfide and convert the zinc oxide and titanium dioxide to zinc titanate within
a reasonable time.
[0051] The following examples are presented in further illustration of the invention.
Example I
[0053] In this example the experimental procedure for the removal of hydrogen sulfide from
gas streams containing less than about 500 ppm of free hydrogen by means of various
solid sorbent materials is described.
[0054] The tests were carried out in a single reactor unit comprising a 20 mm O.D. Quartz
reactor and a 2 mm Thermocouple well. The reactor, which was maintained at a pressure
of about 1.7 psig, was operated in a fixed bed down flow mode using 10 grams of sorbent.
Within the reactor, the sorbent was heated to the reaction temperature in a stream
of nitrogen. When the desired temperature was attained, the nitrogen flow was stopped,
and the simulated sulfur plant gas and, when used, water vapor flows were started.
The water vapor was generated by pumping water through a heated line that was connected
to the top of the reactor. The reaction was carried out at a reaction temperature
of about 538°C and a gas hourly space velocity of 2050 cc/cc catalyst/hour. The composition
of the simulated sulfur plant gas was as follows: 2.1 volume-% hydrogen sulfide, 26.2
volume-% carbon dioxide, and 71.7 volume-% nitrogen.
[0055] The progress of the absorption was followed by measuring the concentration of hydrogen
sulfide and/or the sulfur dioxide in the reactor effluent after the water vapor had
been condensed and removed from the effluent. The concentration of hydrogen sulfide
and/or sulfur dioxide was measured with Draeger tubes that were suited to the concentration
ranges encountered.
[0056] Once the sorbents became fully sulfided, as evidenced by hydrogen sulfide breakthrough,
the flow of the simulated sulfur plant gas to the reactor was halted and the reactor
was purged with nitrogen for a period of about 20 minutes while being heated to a
regeneration temperature of about 632°C. The sulfided sorbent was then regenerated
in the presence of air for about 1.5 hours. Following regeneration, the reactor was
again purged with nitrogen for about 40 minutes while being cooled back down to the
reaction temperature of about 538°C. The nitrogen purge was then halted and the simulated
sulfur plant gas was fed to the reactor to begin another absorption cycle.
Example II
[0057] This example describes the sorbent materials which were tested in accordance with
the procedures set forth in Example I.
[0058] Sorbent A: comprised ZnO/Al₂O₃ with 50 weight-% ZnO and 50 weight-% Al₁O₂. Sorbent A was prepared
in the following manner: First, ZnO powder (Lot 052579; Alfa Products Division, Morton
Thiokol, Inc.; Danvers, MA) was ground to a particle size of -200 mesh. Next, about
61.2 grams of α-alumina monohydrate were dispersed in 500 mL of water with stirring.
4.4 mL of concentrated nitric acid were then added to the solution to form an acidic
solution comprising alumina. Next, a ZnO hydrosol was prepared by slurrying 50.5 grams
of the ground ZnO powder in 150 ml of water. After stirring the acidic solution comprising
alumina for about 10 minutes, the ZnO hydrosol was added, with rapid stirring, to
the acidic solution comprising alumina, and a hydrogel of zinc oxide and alumina was
quickly formed. The hydrogel of zinc oxide and alumina was then transferred to an
evaporating dish and dried at a temperature of about 120°C for about 12 hours. The
dried hydrogel was then calcined in air at 500°C for a period or 3 hours. The BET/N₂
surface area of Sorbent A was about 60 m²/g.
[0059] Sorbent B: comprised Ni/Mo/P/ZnO/Al₂O₃ with 1.08 weight-% Ni (as NiO), 5.40 weight-% Mo (as
MoO₃), 0.57 weight-% P (as P₂O₅), 47.6 weight-% ZnO and 47.6 weight-% Al₂O₃. Sorbent
B was prepared in the following manner: First, a solution of promoting metals was
prepared by combining about 16.4 grams of NiCO₃ (Tech Lot 731215; Fisher Scientific
Company; Pittsburg, PA), about 51.0 grams of MoO₃ (Lot KLNY; Mallinckordt, Inc.; St.
Louis, MO), and about 9.8 grams of H₃PO₄ (85%) (Lot 61257; Merck Sharp & Dohme/Isotopes;
St. Louis, MO) in about 80 mL of deionized water. This solution was refluxed for about
3.5 hours. About 11.0 grams of Sorbent A was then impregnated, by incipient wettness,
with 1.92 grams of the solution of promoting metals and about 3.68 grams of water.
The resulting composition was then dried overnight at a temperature of about 160°C
and, thereafter, calcined in air at 500°C for about 3 hours. The BET/N₂ surface area
of Sorbent B was 55 m²/g.
[0060] Sorbent C: comprised Fe/ZnO/Al₂O₃ with 6.3 weight-% Fe (as Fe₂O₃), 46.8 weight-% ZnO and 46.8
weight-% Al₂O₃. Sorbent C was prepared in the same manner as Sorbent B, except that
3.78 grams of Fe(NO₃)₃ · 9H₂O and 5.0 grams of water were used to impregnate 11.0
grams of Sorbent A.
[0061] Sorbent D: comprised Ni/ZnO/Al₂O₃ with 5.7 weight-% Ni (as NiO), 47.2 weight-% ZnO and 47.2
weight-% Al₂O₃. Sorbent D was prepared in the same manner as Sorbent B, except that
2.60 grams of Ni(HO₁)₂ · 6H₂O and 5.0 grams of water were used to impregnate 11.0
grams of Sorbent A.
[0062] Sorbent E: comprised Cu/ZnO/Al₂O₃ with 4.7 weight-% Cu (as CuO), 47.6 weight-% ZnO, and 47.6
weight-% Al₂O₃. Sorbent E was also prepared in the same manner as Sorbent B, except
that 1.99 grams of Cu(NO₃)₂ · 6H₂O and 5.0 grams of water were used to impregnate
11.0 grams of Sorbent A.
[0063] Sorbent F: comprised Co/ZnO/Al₂O₃ with 4.5 weight-% Co (as CoO), 47.8 weight-% ZnO, and 47.8
weight-% Al₂O₃. Sorbent F was also prepared in the same manner as Sorbent B, except
that 2.59 grams of Co(NO₃)₂ · 6H₂O and 5.0 grams of water were used to impregnate
11.0 grams of Sorbent A.
Example III
[0064] This example illustrates the use of the sorbents described in Example II within the
procedure described in Example I for the removal of H₂S from a simulated sulfur plant
gas. The results are presented as a function of the amount of hydrogen sulfide and
the amount of sulfur dioxide present in the effluent gaseous stream (measured in ppm)
as of the time of the reading. The cycle number listed is the number of the absorption
cycle in which the reading was taken during an ongoing test comprising repeated cycles
of absorption and regeneration. The test results are summarized in Table I.
[0065] A comparison of the results set forth in Table 1 clearly shows that an absorbing
composition promoted only with nickel oxide (Run 4) is superior to other promoters
in absorbing hydrogen sulfide from a fluid stream containing hydrogen sulfide and
less than 500 ppm of free hydrogen without oxidizing significant amounts of the hydrogen
sulfide to sulfur dioxide. In particular, a review of Runs 1-3 and 5-6 shows that
the other promoters were oxidizing a significant amount of the hydrogen sulfide contained
in the fluid stream to sulfur dioxide and then passing the produced sulfur dioxide,
unabsorbed, with the remaining effluent gas.
[0066] While this invention has been described in detail for purposes of illustration, it
is not to be construed as limited thereby but is intended to include all reasonable
variations and modifications within the scope and spirit of the described invention
and the appended claims.
1. A composition consisting essentially of nickel oxide and a base material selected
from the group consisting of zinc oxide and zinc titanate.
2. A composition in accordance with claim 1 wherein the amount of nickel oxide in
said composition is in the range of about 0.1 weight-% to about 15 weight-%, in particular
about 2.0 weight-% to about 73 weight-% said weight-% being expressed in terms of
the nickel oxide based upon the total weight of the composition.
3. A composition in accordance with claim 1 wherein said base material is zinc titanate
and said zinc titanate is prepared by calcining a mixture of zinc oxide and titanium
dioxide in the presence of molecular oxygen at a temperature in the range of about
650°C to about 1050°C.
4. A composition in accordance with claim 3 wherein the atomic ratio of zinc to titanium
in said zinc titanate is in the range of about 1:1 to about 3:1, in particular about
1.8:1 to about 2.2:1.
5. A composition in accordance with claim 1, wherein said base material is zinc oxide
and further comprises alumina.
6. A composition in accordance with claim 5 wherein the amount of alumina in said
composition is in the range of about 10 weight-% to about 50 weight-%, in particular
about 30 weight-% to about 40 weight-%, said weight-%, based upon the total weight
of the composition.
7. A composition in accordance with claim 5 wherein the amount of nickel oxide in
said composition is in the range of about 0.1 weight-% to about 15 weight-%, said
weight-% being expressed in terms of the nickel oxide based upon the total weight
of the composition.
8. A composition in accordance with claim 5 wherein the amount of nickel oxide is
in the range of about 2.0 weight-% to about 7.5 weight-%, and the amount of alumina
in said composition is in the range of about 30 weight-% to about 40 weight-%, based
upon the total weight of the composition.
9. A composition in accordance with one of the claims 5 - 8 wherein said composition
is prepared by one of the following:
A. a process comprising the steps of:
a) mixing zinc oxide or a precursor of zinc oxide, alumina, and nickel oxide or a
precursor of nickel oxide to form a homogeneous mixture thereof;
b) adding a dilute acid to said homogeneous mixture to form a peptized material;
c) drying said peptized material; and,
d) calcining the dried, peptized material to produce said composition
wherein said precursor of zinc oxide is selected from the group consisting of zinc
sulfide, zinc sulfate, zinc hydroxide, zinc carbonate, zinc acetate, and zinc nitrate;
said precursor of nickel oxide is selected from the group consisting of nickel acetates,
nickel carbonates, nickel nitrates, nickel sulfates, nickel thiocyanates, and mixtures
of two or more thereof; said dilute acid is a dilute solution of an acid selected
from the group consisting of nitric acid, acetic acid, sulfuric acid, and hydrochloric
acid; the concentration of said acid in said dilute acid is in the range of about
1.0 weight-% to about 15 weight-% based upon the total weight of the dilute acid;
said peptized material is dried at a temperature in the range of about 75°C to about
300°C for a period of time in the range of about 0.5 hour to about 4.0 hours; and,
said dried, peptized material is calcined in the presence of oxygen at a temperature
in the range of about 375°C to about 750°C for a period of time in the range of about
0.5 hour to about 4.0 hours,
B. or by a process comprising the steps of:
a) mixing zinc oxide, alumina, and nickel oxide or a precursor of nickel oxide to
form a homogeneous mixture thereof;
b) adding dilute acetic acid, having an acid concentration in the range of about 1.0
weight-% to about 5.0 weight-% based upon the total weight of the dilute acid, to
said homogeneous mixture to form a peptized material;
c) drying said peptized material at a temperature in the range of about 90°C to about
250°C for a period of time in the range of about 1 hour to about 2 hours; and,
d) calcining the dried, peptized material in the presence of free oxygen at a temperature
in the range of about 500°C to about 700°C for a period of time in the range of about
1 hour to about 2 hours to produce said composition,
C. or by a process comprising the steps of:
a) mixing zinc oxide or a precursor of zinc oxide with alumina to form a homogeneous
mixture thereof;
b) adding a dilute acid to said homogeneous mixture to form a peptized material;
c) drying said peptized material;
d) calcining the dried, peptized material;
e) adding nickel oxide or a precursor of nickel oxide to the calcined, peptized material
to produce a promoted material;
f) drying said promoted material; and,
g) calcining the dried, promoted material to produce said composition,
wherein said precursor of zinc oxide is selected from the group consisting of zinc
sulfide, zinc sulfate, zinc hydroxide, zinc carbonate, zinc acetate, and zinc nitrate;
said dilute acid is a dilute solution of an acid selected from the group consisting
of nitric acid, acetic acid, sulfuric acid, and hydrochloric acid; the concentration
of said acid in said dilute acid is in the range of about 1.0 weight-% to about 15
weight-% based upon the total weight of the dilute acid; said peptized material is
dried at a temperature in the range of about 75°C to about 300°C for a period of time
in the range of about 0.5 hour to about 4.0 hours; said dried, peptized material is
calcined in the presence of free oxygen at a temperature in the range of about 375°C
to about 750°C for a period of time in the range of about 0.5 hour to about 4.0 hours;
said precursor of nickel oxide is selected from the group consisting of nickel acetates,
nickel carbonates, nickel nitrates, nickel sulfates, nickel thiocyanates, and mixtures
of two or more thereof; said promoted material is dried at a temperature in the range
of about 75°C to about 300°C for a period of time in the range of about 75°C to about
300°C for a period of time in the range of about 0.5 hour to about 8.0 hours; and,
said dried, promoted material is calcined in the presence of free oxygen at a temperature
in the range of about 375°C to about 750°C for a period of time in the range of about
0.5 hour to about 4.0 hours
D. or by a process comprising the steps of:
a) mixing zinc oxide and alumina to form a homogeneous mixture thereof;
b) adding dilute acetic acid, having an acid concentration in the range of about 1.0
weight-% to about 5.0 weight-% based upon the total weight of the dilute acid, to
said homogeneous mixture to form a peptized material;
c) drying said peptized material at a temperature in the range of about 90°C to about
250°C for a period of time in the range of about 1 hour to about 2 hours;
d) calcining the dried, peptized material in the presence of free oxygen at a temperature
in the range of about 500°C to about 700°C for a period of time in the range of about
1 hour to about 2 hours;
e) adding nickel oxide or a precursor of nickel oxide to the calcined, peptized material
to produce a promoted material;
f) drying the promoted material at a temperature in the range of about 90°C to about
250° C for a period of time in the range of about 3 hours to about 5 hours;
g) calcining the dried, promoted material in the presence of free oxygen at a temperature
in the range of about 500°C to about 700°C for a period of time in the range of about
1 hour to about 2 hours to produce said composition.
10. A composition in accordance with claim 1 wherein said base material is zinc titanate
and further comprises alumina.
11. A composition in accordance with claim 10 wherein the amount of alumina in said
composition is in the range of about 10 weight-% to about 50 weight-% in particular
in the range of about 30 weight-% to about 40 weight-%, based upon the total weight
of the composition.
12. A composition in accordance with claim 10 wherein the amount of nickel oxide in
said composition is in the range of about 0.1 weight-% to about 15 weight-%, said
weight-% being expressed in terms of the nickel oxide based upon the total weight
of the composition.
13. A composition in accordance with claim 10 wherein the amount of nickel oxide is
in the range of about 2.0 weight-% to about 7.5 weight-%, and the amount of alumina
in said composition is in the range of about 30 weight-% to about 40 weight-%, based
upon the total weight of the composition.
14. A composition in accordance with claim 10 wherein said zinc titanate is prepared
by calcining a mixture of zinc oxide and titanium dioxide in the presence of molecular
oxygen at a temperature in the range of about 650°C to about 1050°C, wherein the atomic
ratio of zinc to titanium in said zinc titanate is in the range of about 1:1 to about
3:1, in particular in the range of about 1.8.:1 to about 2.2:1.
15. A composition in accordance with claim 10 wherein said composition is derived
from a hydrogel comprising zinc titanate and alumina, in particular having been prepared
by calcining a mixture of zinc oxide and titanium dioxide in the presence of free
oxygen at a temperature in the range of about 650°C to about 1050°C to form zinc titanate,
mixing the thus formed zinc titanate in a powdered form with hydrosol of alumina hydrate
to form a zinc titanate and alumina hydrosol, adding ammonium hydroxide to convert
said hydrosol to a hydrogel, drying said hydrogel at a temperature in the range of
about 35°C to about 150°C for a period of time in the range of about 8 hours to about
24 hours and calcining said hydrogel in the presence of free oxygen at a temperature
in the range of about 425°C to about 650°C for a time of about 2 hours to form a hydrogel
derived composition of zinc titanate and alumina, adding nickel oxide or a precursor
of nickel oxide to said hydrogel derived composition of zinc titanate and alumina,
drying said hydrogel derived composition of zinc titanate and alumina to which nickel
oxide or a precursor of nickel oxide has been added at a temperature in the range
of about 70°C to about 130°C for a period of time in the range of about 0.5 hour to
about 8 hours, and calcining the dried hydrogel derived composition of zinc titanate
and alumina to which nickel oxide or a precursor of nickel oxide has been added in
the presence of free oxygen at a temperature in the range of about 375°C to about
650°C for a time in the range of about 0.5 hours to about 4.0 hours to form said hydrogel
derived composition.
16. A process for removing hydrogen sulfide from a fluid stream containing hydrogen
sulfide and less than 500 ppm of free hydrogen comprising the step of contacting said
fluid stream under suitable absorbing conditions with an absorbing composition as
defined in one of the claims 1 to 15.
17. A process in accordance with claim 16 wherein said suitable absorbing conditions
comprise a temperature in the range of about 150°C to about 600°C, a total system
pressure in the range of about atmospheric to about 2000 psig, and a residence time
for said fluid stream in the presence of said absorbing composition in the range of
about 10 to about 10,000 volumes of gas at standard temperature and pressure per volume
of said absorbing composition per hour.
18. A process in accordance with claim 16 or 17 additionally comprising the steps
of:
discontinuing the flow of said fluid stream over said absorbing composition; and
contacting said absorbing composition, after the flow of said fluid stream is discontinued,
with a free oxygen-containing gas under suitable regeneration conditions to thereby
regenerate said absorbing composition.
19. A process in accordance with claim 18 wherein said suitable regeneration conditions
comprise a feed rate of said free oxygen-containing gas suitable to supply sufficient
oxygen to remove substantially all of the sulfur from said absorbing composition as
an oxide a temperature in the range of about 370°C to about 815°C, and a pressure
of about atmospheric.
20. A process in accordance with claim 18 additionally comprising the step of purging
said absorbing composition with an inert fluid after the step of discontinuing the
flow of said fluid stream and before the step of contacting said absorbing composition
with a free oxygen-containing fluid.
21. A process in accordance with claim 18 additionally comprising the steps of:
terminating the flow of said free oxygen-containing gas over said absorbing composition
after said absorbing composition is substantially regenerated; purging said absorbing
composition with an inert fluid after the flow of said free oxygen-containing gas
is terminated;
terminating the flow of said inert fluid over said absorbing composition after said
free oxygen-containing gas is substantially purged from said absorbing composition;
and
recontacting said absorbing composition with said fluid stream after the flow of said
inert fluid is terminated.